Botanical Oil Extraction Method and System

ABSTRACT

A method and apparatus for extracting botanical oil from botanical mass includes milling the biomass and chilling the milled biomass. The biomass is then exposed to a chilled ethanol solvent. Water is added and the solution introduced into a first centrifuge. The clean ethanol slurry is then introduced into an evaporator leaving a two-phase mixture which is introduced into a second centrifuge which separates the water from the pure botanical oil.

CROSS-REFERENCE TO RELATED APPLICATIONS

This non-provisional patent application is a continuation application ofU.S. application Ser. No. 14/780,528 filed Feb. 3, 2020, which claimspriority to U.S. Provisional Application Ser. No. 62/802,240 filed Feb.7, 2019, U.S. Provisional Application Ser. No. 62/801,671 filed Feb. 6,2019, and U.S. Provisional Application Ser. No. 62/801,672 filed Feb. 6,2019, the disclosures of which are incorporated by reference herein intheir entirety.

STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH OR DEVELOPMENT

Not applicable.

BACKGROUND OF THE INVENTION Field of the Invention

This invention is directed to a method and system for extractingbotanical oil from botanical biomass.

Description of Related Arts

There are many well know mechanical and solvent based extractionsmethods to extract botanical oil from botanical biomass. For example;mechanically induced forces can be an effective mechanical extractionmethod at certain temperatures and pressures. Supercritical carbondioxide can be an effective solvent extraction method when utilized atcertain temperatures and pressures. Hydrocarbons such as butane andhexane can be an effective solvent extraction method when utilized atcertain temperatures and pressures. Ethanol can be an effective solventextraction method when utilized at certain temperatures and pressures.While all of these can be effective extraction methods of extractingbotanical oil from botanical biomass, none of these extraction methodsproduce a pure botanical oil principally free of undesirable botanicalbiomass.

Ethanol solvent extractions processes are considered to be a veryefficient means of extracting botanical oil. It is also a very scalableprocess and has one of the highest extraction rates per square foot ofspace of any extraction process currently utilized within the industry.However, the highly polar nature of ethanol results in the extraction ofundesirable biomass if the extraction process variables are notsufficiently controlled. Current technology utilized within the industrydoes not provide for a means of precisely controlling the variables ofthe ethanol solvent extraction process to sufficiently prevent theextraction of undesirable biomass.

Therefore, there is a need for a safe and efficient ethanol solventextraction process of botanical oil from botanical biomass that providesfor precisely controlling the variables of the ethanol solventextraction process to sufficiently prevent the extraction of undesirablebotanical biomass.

The present invention addresses these and other needs by providing asystem and method for safely, efficiently and precisely controlling thevariables of the ethanol solvent extraction process.

BRIEF SUMMARY OF THE INVENTION

The botanical biomass is first subject to a milling process toeffectively increase the surface area to volume ratio (SA:V) of the bulkbotanical biomass. The milled botanical biomass is then exposed to aheat transfer process to remove heat from and thus reduce thetemperature of the botanical biomass. The now chilled botanical biomassis introduced into the extractor where it is exposed to chilled ethanolsolvent. The botanical oil and other solubles of the botanical biomassare solvated into solution with the chilled ethanol solvent and aredischarged as a liquid solution from the extractor. The remainingbotanical biomass is discharged separately as a solid for disposal.Water is added to the chilled ethanol solution causing the solids insolution to precipitate forming a chilled ethanol slurry. The slurry isthen introduced into a centrifuge where it is exposed to an elevatedcentripetal force to remove principally all of the remaining undesirablebotanical biomass. The clean ethanol solution is then introduced into anevaporator where the ethanol is removed from the solution as a vaporleaving a two-phase liquid mixture consisting of clean botanical oil andwater. The multi-phase liquid mixture is then introduced into a secondcentrifuge where it is exposed to an elevated centripetal force toseparate the two phases of the multi-phase liquid. The now separatedwater is disposed of leaving the now separated clean and pure botanicaloil.

The following detailed description and drawings of the preferredembodiment of the Botanical Oil Extraction Method and System is intendedas an exemplification of the principals of the invention and notintended to limit the invention to any specific embodiment.

BRIEF DESCRIPTION OF THE DRAWINGS

For a detailed description of the preferred embodiment of the invention,reference will be made to the accompanying drawing. FIG. 1 is aschematic showing of a system according to a first embodiment of theinvention.

DETAILED DESCRIPTION OF AN EMBODIMENT

FIG. 1 depicts flow diagram 100 of the process of this invention. Flowdiagram 100 includes feed hopper 110 including outlet 120. Outlet 120 offeed hopper 110 is mechanically coupled to and in conveyancecommunication with Inlet 130 of pre-screener 140. Outlet 150 ofpre-screener 140 is mechanically coupled to and in conveyancecommunication with inlet 180 of Miller 190 via variable speed feed screw170 (i.e., Screw Conveyor). Outlet 200 of Miller 190 is mechanicallycoupled to and in pneumatic communication with inlet 230 of divertervalve 260. Outlet 240 of diverter valve 260 is mechanically coupled toand in pneumatic communication with inlet 270 of heat exchanger 280.Outlet 290 of heat exchanger 280 is mechanically coupled to and inpneumatic communication with Screw Conveyor 170.

Outlet 250 of diverter valve 260 is mechanically coupled to and inpneumatic communication with feed screw 300 (i.e., feed conveyor). Feedconveyor 300 is mechanically coupled to and in conveyance communicationwith inlet 310 of extractor 330. Outlet 340 of extractor 330 ismechanically coupled to and in fluid communication with inlet 360 of pd(positive displacement) pump 370. Outlet 380 of pd pump 370 ismechanically coupled to and in fluid communication with inlet 390 ofmixing valve 400. Outlet 420 of mixing valve 400 is mechanically coupledto and in fluid communication with inlet 490 of centrifuge 500. Outlet520 of centrifuge 500 is mechanically coupled to and in fluidcommunication with inlet 530 of evaporator 540. Outlet 560 of evaporator540 is mechanically coupled to and in fluid communication with inlet 600of centrifuge 610. Outlet 630 of centrifuge 610 is mechanically coupledto and in fluid communication with inlet 640 of pd pump 650. Outlet 660of pd pump is mechanically coupled to and in fluid communication withthe clean botanical oil outlet.

Outlet 550 of evaporator 540 is mechanically coupled to and in fluidcommunication with inlet 570 of pd pump 580. Outlet 590 of pd pump 580is mechanically coupled to and in fluid communication with inlet 480 ofbuffer tank 470. Outlet 460 of buffer tank 470 is mechanically coupledto and in fluid communication with inlet 450 of pd pump 440. Outlet 430of pd pump 440 is mechanically coupled to and in fluid communicationwith inlet 320 of extractor 330.

Outlet 620 of centrifuge 610 is mechanically coupled to and in fluidcommunication with inlet 670 of pd pump 680. Outlet 690 of pd pump 680is mechanically coupled to and in fluid communication with inlet 700 ofbuffer tank 720. Buffer tank 720 also includes inlet 710 mechanicallycoupled to and in fluid communication with a fresh water supply. Outlet730 of buffer tank 720 is mechanically coupled to and in fluidcommunication with inlet 740 of pd pump 750. Outlet 760 of pd pump 750is mechanically coupled to and in fluid communication with inlet 410 ofmixing valve 400.

Outlet 510 of centrifuge 500 is mechanically coupled to and inconveyance communication with inlet 770 of receiving bin 780.

Outlet 350 of extractor 330 is mechanically coupled to and in conveyancecommunication with inlet 770 of receiving bin 780. Inlet 770 ofreceiving bin 780 is of a “T” design.

Outlet 160 of pre-screener 140 is mechanically coupled to and inconveyance communication with inlet 210 of receiving bin 220.

Again, referring to FIG. 1. and now describing in detail a preferredmethod of the invention.

Botanical biomass is introduced into feed hopper 110 at inlet 101 offeed hopper 110. Feed hopper 110 is mechanically coupled to and inconveyance communication with inlet 130 of pre-screener 140 where thebotanical biomass is pre-screened to remove undesirables. Thepre-screened botanical biomass is discharged at outlet 150 ofpre-screener 140 that is mechanically coupled to and in conveyancecommunication with Screw Conveyor 170. Screw conveyor 170 ismechanically coupled to and in conveyance communication with inlet 180of Miller 190.

Miller 190 is a component of a system that includes heat exchanger 280and diverter valve 260, said system taught in U.S. provisional patentapplication Ser. No. 62/801,672 filed Feb. 6, 2019, the entire contentsof which is expressly incorporated herein by reference thereto.

The system that includes Miller 190, heat exchanger 280 and divertervalve 260 each mechanically coupled and in pneumatic communication thusforming a pneumatic circulation loop whereby botanical biomass fed intoinlet 180 of Miller 190 will be pneumatically conveyed through Miller190 where a portion of the botanical biomass surface area will beincreased as the botanical biomass is then discharged at outlet 200 ofMiller 190. The botanical biomass is then received at inlet 230 ofdiverter valve 260 where diverter valve 260 is configured to dischargeat outlet 240 and then received at inlet 270 of heat exchanger 280. Heatexchanger 280 removes a portion of the heat, sensible and latent, beforedischarging the chilled botanical biomass at outlet 290 into ScrewConveyor 170 at the point of interface with inlet 180 of Miller 190.

The just described system allows for the botanical biomass to becontinuously circulated in a dilute phase within the system with eachcirculation increasing the SA:V ratio and reducing the temperature ofthe botanical biomass. After a predetermined period of time, sufficientto adequately increase the SA:V ratio of the bulk botanical biomass to avalue greater than 500:1 and remove sufficient heat to reduce thetemperature to less than 32° F., diverter valve 260 is configured todischarge at outlet 250 of diverter valve 260. Outlet 250 of divertervalve 260 is mechanically coupled to and in pneumatic communication withfeed conveyor 300 and thereby chilled botanical biomass is received intofeed conveyor 300. Feed conveyor 300 is mechanically coupled to and inconveyance communication with inlet 310 of extractor 330. Feed conveyor300 is of a variable speed configuration allowing feed conveyor 300 toregulate the conveyance rate of chilled botanical biomass into inlet 310of extractor 330.

Extractor 330 disclosed herein is the apparatus taught in U.S.provisional patent application Ser. No. 62/801,671 filed Feb. 6, 2019,the entire contents of which is expressly incorporated herein byreference thereto.

Chilled botanical biomass received at inlet 310 of extractor 330 isintroduced onto the interior surface of the rotating cylindrical screenof extractor 330. The rotating speed of the rotating cylindrical screenof extractor 330 is variable. The initial rotating speed of the rotatingcylindrical screen of extractor 330 results in a centripetal force equalto less than 1 g during the period where chilled botanical biomass isintroduced onto the interior surface of the rotating cylindrical screenof extractor 330 to a predetermined level. Chilled ethanol solvent isintroduced onto the interior surface of the rotating cylindrical screenat inlet 320 of extractor 330, inlet 320 of extractor 330 is of a flatspray nozzle design located near the axis of rotation of the rotatingcylindrical screen of extractor 330. Chilled ethanol solvent isintroduced concurrent with and subsequent to the introduction of thechilled botanical biomass onto the interior surface of the rotatingcylindrical screen of extractor 330. The introduction of chilled ethanolsolvent will continue for a period of time and in a quantity sufficientto solvate a predetermined amount of the chilled botanical biomass andother soluble constituents of the chilled botanical biomass forming asolution comprising of the chilled ethanol solvent and the solvatedconstituents of the chilled botanical biomass. The solution iscontinuously filtered through the rotating cylindrical screen ofextractor 330 at a rate determined by the rotating speed of the rotatingcylindrical screen of extractor 330.

As previous disclosed the rotating speed of rotating cylindrical screenof extractor 330 is variable. This feature of the rotating cylindricalscreen of extractor 330 allows the screen to rotate at a speed resultingin a centripetal force equal to less than 1 g and then at a higher rateof speed resulting in a centripetal force significantly greater than 1g.

In one example of a preferred method, the rotating cylindrical screen ofextractor 330 is first operated at less than 1 g. This will result in atumbling action of the chilled botanical biomass as the rotatingcylindrical screen of extractor 330 rotates. Additionally, the chilledethanol solvent that is simultaneously introduced onto the interiorsurface of the rotating cylindrical screen of extractor 330, at inlet320 of extractor 330, and onto the inner annular formed by the tumblingchilled botanical biomass, will tend to remain in contact with thechilled botanical biomass keeping the chilled botanical biomass wet withchilled ethanol solvent. This process will continue for a period of timesufficient to elevate the level of solvated chilled botanical biomasswithin the chilled ethanol solvent to approximately 50% of the totalsolubility of the soluble chilled botanical biomass within the chilledethanol solvent, thus creating a chilled ethanol solution.

Subsequently, the rotating speed of the rotating cylindrical screen ofextractor 330 will be increased sufficiently enough to cause the chilledethanol solution to drain from the surface and subsurface of the chilledbotanical biomass. Subsequent to the draining process where the rotatingcylindrical screen of extractor 330 is rotating at a speed resulting ina centripetal force significantly greater than 1 g, the rotatingcylindrical screen of extractor 330 is slowed to a rotating speed thatresults in a centripetal force of less than 1 g. This cyclic processwhere the chilled botanical biomass first wetted with principally cleanchilled ethanol solvent and then subsequently dried of the resultingchilled ethanol solution will be repeated a number of times sufficientto solvate principally all of the soluble desirable constituents of thechilled botanical biomass. The chilled ethanol solution drained from thechilled botanical biomass is filtered as it moves from the inner surfaceof the rotating cylindrical screen of extractor 330 to the outer surfaceof the rotating cylindrical screen of extractor 330 where it isseparated from the rotating cylindrical screen by centripetal force andis received into the integrated chilled ethanol solution receiving tankof extractor 330.

The integrated chilled ethanol solution receiving tank of extractor 330includes outlet 340 of extractor 330. Outlet 340 of extractor 330 ismechanically coupled to and in fluid communication with inlet 360 of pdpump 370. The chilled ethanol solution discharged at outlet 340 ofextractor 330 is received at inlet 360 of pd pump 370. Outlet 380 of pdpump 370 is mechanically coupled to and in fluid communication withintake 390 of mixing valve 400. The chilled ethanol solution isdischarged under pressure at outlet 380 of pd pump 370 to be received atinlet 390 of mixing valve 400. Mixing valve 400 features two inlets(inlet 390 and inlet 410) and one outlet (outlet 420). Chilled ethanolsolution received at inlet 390 of mixing valve 400 is mixed with waterreceived at inlet 410 of mixing valve 400 at a ratio that results inoversaturation of the ethanol within the chilled ethanol solutioncausing the undesirable constituents of the chilled ethanol solution toprecipitate thus creating a chilled ethanol slurry discharged at outlet420 of mixing valve 400.

Outlet 420 of mixing valve 400 is mechanically coupled to and in fluidcommunication with inlet 490 of centrifuge 500. The chilled ethanolslurry is received at inlet 490 of centrifuge 500. In the preferredembodiment of this invention, centrifuge 500 is of a stacked disc,self-cleaning, separator design. This stacked disc, self-cleaning,separator design, is capable of developing a very large centripetalforce. The chilled ethanol slurry received at inlet 490 of centrifuge500 is exposed to a sufficient amount of centripetal force for asufficient amount of time to settle the precipitate to the inner wall ofthe rotating element of centrifuge 500. The wall of the rotating elementof centrifuge 500 features a valve that is opened hydraulically duringoperation to allow the precipitate to be discharged at outlet 510 ofcentrifuge 500. This feature allows for continuous operation ofcentrifuge 500 without the need to suspend the operation of centrifuge500 for removal of the precipitate from the inner wall of the rotatingelement of centrifuge 500. The chilled ethanol solution, now principallyfree from precipitate, is discharged at outlet 520 of centrifuge 500.

Outlet 520 of centrifuge 500 is mechanically coupled to and in fluidcommunication with inlet 530 of evaporator 540. The chilled ethanolsolution discharged from outlet 520 of centrifuge 500 is received atinlet 530 of evaporator 540. Alternatively, the chilled ethanol solutiondischarged from outlet 380 of pd pump 370 is received at inlet 530 ofevaporator 540. In an embodiment of this invention, evaporator 540 is ofa falling film, concurrent design. Chilled ethanol solution received atinlet 530 of evaporator 540 is subject to environmental conditions andmechanical interfaces that result in repetitive evaporation andcondensing cycles. These cycles effectively separate the ethanol fromthe chilled ethanol solution. The separated ethanol is discharged fromoutlet 550 of evaporator 540. The remaining mixture, principallycontaining water and botanical oil, is discharge at outlet 560 ofevaporator 540.

Outlet 560 of evaporator 540 is mechanically coupled to and in fluidcommunication with inlet 600 of centrifuge 610. The chilled ethanolsolution discharged at outlet 560 of evaporator 540 is received at inlet600 of centrifuge 610. Centrifuge 610 is of a stacked disc, clarifierdesign and is capable of developing a very large centripetal force andis very efficient at separating the botanical oil from the water wherethe botanical oil is discharged at outlet 630 of centrifuge 610 and thewater is discharged at outlet 620 of centrifuge 610.

Outlet 630 of centrifuge 610 is mechanically coupled to and in fluidcommunication with inlet 640 of pd pump 650. Clean botanical oilprincipally free of water, precipitate, and other undesirables isdischarged at outlet 630 of centrifuge 610 and received at inlet 640 ofpd pump 650. The clean botanical oil is discharged under pressure atoutlet 660 of pd pump 650 for further transfer down line.

Outlet 550 of evaporator 540 is mechanically coupled to and in fluidcommunication with inlet 570 of pd pump 580. Ethanol discharged atoutlet 550 of evaporator 540 is received at inlet 570 of pd pump 580.Ethanol discharged under pressure at outlet 590 of pd pump 580 isreceived at inlet 480 of buffer tank 470.

Outlet 460 of buffer tank 470 is mechanically coupled to and in fluidcommunication with inlet 450 of pd pump 440. Ethanol is discharged underpressure at outlet 430 of pd pump 440 and received at inlet 320 ofextractor 330.

Inlet 320 of extractor 330 is of a flat spray nozzle design.

Outlet 620 of centrifuge 610 is mechanically coupled to and in fluidcommunication with inlet 670 of pd pump 680. Water discharged at outlet620 of centrifuge 610 is received at inlet 670 of pd pump 680. Waterdischarged under pressure at outlet 690 of pd pump 680 is received atinlet 700 of buffer tank 720. Buffer tank 720 features inlet 710. Makeup water to compensate for process losses is received at inlet 710 ofbuffer tank 720.

Outlet 730 of buffer tank 720 is mechanically coupled to and in fluidcommunication with inlet 740 of pd pump 750. Water discharged at outlet730 of buffer tank 720 is received at inlet 740 of pd pump 750. Outlet760 of pd pump 750 is mechanically coupled to and in fluid communicationwith inlet 410 of mixing valve 400. Water is discharged under pressureat outlet 760 of pd pump 750 in sufficient quantities to meet the demandof mixing valve 400.

Outlet 510 of centrifuge 500 is mechanically coupled to and inconveyance communication with inlet 770 of Receiver Bin 780. Inlet 770of Receiver Bin is of a “T” design. Precipitate and associated attachedliquid discharged at outlet 510 of centrifuge 500 is received at inlet770 of receiving bin 780.

Outlet 350 of extractor 330 is mechanically coupled to and in conveyancecommunication with inlet 770 of Receiver Bin 780. Spent botanicalbiomass and associated attached liquid discharged at outlet 350 ofextractor 330 is received at inlet 770 of receiving bin 780.

Outlet 160 of pre-screener 140 is mechanically coupled to and inconveyance communication with inlet 210 of receiving bin 220.Undesirable overflow from the screen of pre-screener 140 is dischargedat outlet 160 of pre-screener 140 and received at inlet 210 of receivingbin 220.

Utilizing the new and unique features of the current invention providesfor a fully automatic method and system to control the extractionvariables associated with solvent type extraction methods, moreparticularly the variables associated with ethanol extractions ofbotanical oils, thereby significantly increasing safety, and efficiencywhile dramatically reducing cost.

Although the present invention and its advantages have been described indetail, it should be understood that various changes, substitutions andalterations may be made herein without departing from the spirit andscope of the invention as defined by the appended claims.

What is claimed is:
 1. A system for extracting botanical oil frombotanical biomass comprising: a feed hopper configured to receivebotanical biomass; a pre-screener that receives the botanical biomassfrom the feed hopper and removes undesirable materials from thebotanical biomass to provide pre-screened botanical biomass; a millingsystem comprising a miller, a diverter valve, and a heat exchanger thatreceives the pre-screened botanical biomass from the pre-screener andcirculates the pre-screened botanical biomass through the miller, thediverter valve, and the heat exchanger to provide a chilled botanicalbiomass, wherein the miller increases the surface area of thepre-screened botanical biomass, wherein the diverter valve controls flowof the pre-screened botanical biomass, and wherein the heat exchangerremoves heat from the pre-screened botanical biomass; an extractor thatreceives the chilled botanical biomass from the milling system via thediverter valve and introduces a solvent onto the chilled botanicalbiomass to solvate at least a portion of the chilled botanical biomassto provide at least a spent portion of the chilled botanical biomass anda botanical biomass solution; a mixing valve that receives the botanicalbiomass solution from the extractor and introduces water into thebotanical biomass solution to cause other undesirable materials of thebotanical biomass solution to precipitate and provide a botanicalbiomass slurry; a first centrifuge that receives the botanical biomassslurry from the mixing valve and removes at least a portion of theprecipitated undesirable materials from the botanical biomass slurry viacentripetal force to provide a second botanical biomass solution; anevaporator that receives the second botanical biomass solution from thefirst centrifuge and separates the solvent from the second botanicalbiomass solution to provide a mixture comprising at least the water andbotanical oil; a second centrifuge that receives the mixture from theevaporator and removes at least a portion of the water from the mixturevia centripetal force to isolate the botanical oil.
 2. The system ofclaim 1, wherein the undesirable materials from the botanical biomass isdischarged to a receiving bin.
 3. The system of claim 1, wherein thespent portion of the chilled botanical and associated attached liquid isdischarged to a receiving bin.
 4. The system of claim 1, wherein theprecipitated undesirable materials and associated attached liquid isdischarged to a receiving bin.
 5. The system of claim 1, wherein thesolvent separated from the second botanical biomass solution is recycledfor use by the extractor.
 6. The system of claim 1, wherein the waterremoved from the mixture is recycled for use by the mixing valve.
 7. Thesystem of claim 1, further comprising one or more feed screws tofacilitate conveyance of the pre-screened botanical biomass, the chilledbotanical biomass, or a combination thereof.
 8. The system of claim 1,further comprising one or more positive displacement pumps to facilitateconveyance of the botanical biomass solution, the solvent, the water,the botanical oil, or any combinations thereof.
 9. The system of claim1, further comprising one or more buffer tanks to compensate for processlosses in the solvent, the water, or a combination thereof.
 10. Thesystem of claim 1, wherein the milling system circulates thepre-screened botanical biomass for a period of time sufficient toincrease surface area to volume ratio of the pre-screened botanicalbiomass to a value greater than 500 to
 1. 11. The system of claim 1,wherein the milling system circulates the pre-screened botanical biomassfor a period of time sufficient to reduce temperature of thepre-screened botanical biomass to less than 32° F.
 12. The system ofclaim 1, wherein the extractor tumbles the chilled botanical biomass andintroduces the solvent composition onto the chilled botanical biomassfor a period of time sufficient to elevate the solvated chilledbotanical biomass within the solvent to approximately 50% of totalsolubility of the chilled botanical biomass.
 13. The system of claim 1,wherein the first and second centrifuges each have a stack disc,self-cleaning, separator design.
 14. The system of claim 1, wherein theevaporator has a falling film, concurrent design.
 15. The system ofclaim 1, wherein the solvent introduced to the chilled botanical biomassand separated from the second botanical biomass solution is ethanol. 16.A system for extracting botanical oil from botanical biomass comprising:a feed hopper configured to receive botanical biomass; a pre-screenerthat receives the botanical biomass from the feed hopper and removesundesirable materials from the botanical biomass to provide pre-screenedbotanical biomass; a milling system comprising a miller, a divertervalve, and a heat exchanger that receives the pre-screened botanicalbiomass from the pre-screener and circulates the pre-screened botanicalbiomass through the miller, the diverter valve, and the heat exchangerto provide a chilled botanical biomass, wherein the miller increases thesurface area of the pre-screened botanical biomass, wherein the divertervalve controls flow of the pre-screened botanical biomass, and whereinthe heat exchanger removes heat from the pre-screened botanical biomass;an extractor that receives the chilled botanical biomass from themilling system via the diverter valve and introduces a solvent onto thechilled botanical biomass to solvate at least a portion of the chilledbotanical biomass to provide at least a spent portion of the chilledbotanical biomass and a botanical biomass solution comprising at leastthe solvent and botanical oil; an evaporator that receives the botanicalbiomass solution from the extractor and separates the solvent from thebotanical biomass solution to isolate the botanical oil.
 17. The systemof claim 16, wherein the milling system circulates the pre-screenedbotanical biomass for a period of time sufficient to increase surfacearea to volume ratio of the pre-screened botanical biomass to a valuegreater than 500 to
 1. 18. The system of claim 16, wherein the millingsystem circulates the pre-screened botanical biomass for a period oftime sufficient to reduce temperature of the pre-screened botanicalbiomass to less than 32° F.
 19. The system of claim 16, wherein theextractor tumbles the chilled botanical biomass and introduces thesolvent composition onto the chilled botanical biomass for a period oftime sufficient to elevate the solvated chilled botanical biomass withinthe solvent to approximately 50% of total solubility of the chilledbotanical biomass.
 20. The system of claim 16, wherein the solventintroduced to the chilled botanical biomass and separated from thebotanical biomass solution is ethanol.